Isomerization of hydrocarbons



,April6,1948. T.B.HuDsoNEr AL 2,4 9,30

18 OMERI ZAT I 0N OF HYDRO CARBONS Filed Oct. 5, 1942 2 Sheets-Sheet 1' ISOMERIZATION 1e PRODUCTS v CHAMBER 22 /CATALYST HYDROCARBON FEED CATALYST 3 '/MAKE-UP Q SPENT 42 MATERIAL INVENTORS THOMAS E. HUDSON JOHN D. UPHAM April 6, 1948. T. B. HUDSON El AL 2,439,301

ISOMERIZATION HYDROCARBONS Filed Oct. 5, 1942 2 Sheets-Sheet 2 Patented Apr. 6, 1948 UNITED STATES PATENT OFFICE ISOMERIZATION OF HYDROGARBONS Thomas B. Hudson and John D. Upham, Bartlesville, kla., assignors .to Phillips Petroleum Company, a corporation of Delaware Application October 5, 1942, Serial No. 460,852

Claims. 1

This invention relates to the catalytic isomerization of hydrocarbons, particularly the lower boiling saturated hydrocarbons such as the paraffins and the cycloparaffins or naphthenes. It has particular application to the formation of branched chain paraflins from less-branched or straight chain parafifiins of the same molecular weight, wherein a mobile isomerization catalyst is utilized.

Isomerization of hydrocarbons has become an important industrial process because of the increased tendency toward high octane number motor fuels, and the development of special uses for certain individual hydrocarbons or groups of hydrocarbons. Thus, the lsoparaffins are ordinarily much more valuable than the normal paraffins, both for use per se, and as stock for manufacturing other hydrocarbons by alkylation, dehydrogenation followed by polymerization, or other conversion processes. One of the most important commercial isomerization processes at the present time is the formation of isobutane from normal butane, using aluminum chloride catalysts. Accordingly, we shall describe our invention with particular reference to such a process, and its application to other isomeriza tions, and/or other catalysts, will be obvious to those skilled in the art in view of the present disclosure.

The isomerizations with which this invention is concerned are equilibrium reactions; that is, at a given temperature the percentageof each of the individual isomers in a mixture of isomers is fixed if equilibrium is attained. For example, if either pure normal butane or pure isobutane be contacted with a suitable catalyst, such as aluminum chloride, under given temperature and pressure conditions permitting the reaction to proceed but preferably avoiding side reactions such as cracking, after a period of time an equilibrium mixture of normal and isobutane will be formed. In this mixture, the-percentage of isobutane will be the same regardless of whether the charging stock was isobutane or normal butane. This means that in isomerizing normal butane to produce isobutane, there is a maximum conversion obtainable at any given temperature. The lower temperatures give the greatest conversion, but too low a temperature cannot be used because the reaction rate will decrease to an uneconomic level. On the other hand, higher temperatures give higher reaction rates, but the equilibrium mixture contains less isobutane. Furundesired side reactions, particularly cracking.

While the percentage yield of isobutane equilibrium is dependent only on temperature, the rate of reaction is dependent on temperature and also on other important factors, including relative concentration of normal and isoloutane in the mixture at the given time, catalyst activity, and the amount of catalyst surface contacted by the butane, or in other words, on the time of contact of a unit volume of butane wit a unit of catalyst activity.

A large surface area for a given weight of active catalytic material may be obtained by various expedients which are well known in the art.

' For instance, inert carriers or extenders may be impregnated by or mixed m'th the catalyst, or the catalyst may be produced in a porous form, or prepared in a condition of fine subdivision as in the use of small grains or powdered catalyst, which may be suspended in liquid or gaseous hydrocarbons undergoing isomerization.

The amount of catalyst surface contactedwith reactants is also dependent on the concentration'of catalyst in reactants, that is, the amount of catalyst, of whatever kind, mixed with the reactants, or placed in a stationary bed or cata lyst through which the reactants pass,a'nd on the flow rate of reactants through a reaction zone.

Thus it is seen that a number of different reaction conditions influence the rate of reaction,

and these reaction conditions frequently vary from point to point in the reaction zone. As the conversion of normal to isobutane occurs in an isomerization zone through which the hydrocarbons are flowing, the decrease in concentration of the normal butane and corresponding increase in concentration of isobutane tends to slow the reaction, particularly as equilibrium is approached. Due to the exothermic nature of this reaction, the temperature has a tendency to in-- process for the catalytic isomerlzation of hydro carbons. Another object is to provide an improved method of contacting catalysts with saturated hydrocarbons to promote molecular rearrangement thereof. A primary object is to correlate the ratio of catalyst activity to reactants throughout an isomerization zone with varying reaction conditions therein so as to maintain carbons, improved catalyst life, and other bene- -rii fits. A further object is to provide. improved methods for carrying out isomerization reactions" involving a primary catalystgand apromotem-z wherein a temperature gradientiexistsu Yetan-v of such catalysts. novel methods of conducting isomerization reactions with gaseous,-liquid, and/or solid-catalysts, wherein-said catalystsareintroduced multipoint into 1a reaction zone; I Other. objects .and advan--' tages, will become apparent! as the disclosure pro ceeds.

the quantity and/or activity of the catalyst;in-=

troduced-at. each point being co-rrelatedvwith the reaction-.-;conditions prevailing at that point. Either concurrent-or;countercurrent flow of catalyst and reactants may be-used,--depending upon the conditions'and the type of catalyst usecL: Thecatalyst may be miscible with, or immiscible with the; reactants. The Variousmodes of operating in accordance With-ourinvention are-not exact equivalents, but may be carried outby one skilled in the art-by following the basic principles disclosed. herein. 1

The accompanying drawings are provided to better explain the invention, and taken in con junction. with the description thereof, will serve to-- exemplify the invention-.- Figure 1-- shows =in semi-diagrammatic form suitableapparatus forcarrying out -the vapor phase isomerization -of normal butane, using a fluid melt type ofaluminum chloride; catalyst, wherein the tempera-- ture of the reactant =-increases during passage through the reaction zone due-to theexothermic nature-oi the reaction. Figure Zshows-in semidiagrammatic form: aseries of-isomerization zones with associated equipment for efiecting isomerizationin the liquid phase.- with a decreasing temperature gradient to obtain maximum equilibrium yields of lisobutane from normal butane.

In: Figure 1,. the reaction chambersl i] comprises i a, ceramicqlinedvertical tower packed with ceramicvware Rasohig ringssstones ortother suitablemeans-for eiitectingdntimate contact between re-- actants andvliquid catalystl The gaseousisomerization: feed which led-linto-reactor id through lined-Z comprises normal butane; either purelor admixed with minor amounts otisobutane, propane -hydrogen, or other lightgases, and anhy-- drous hydrogen chloride which acts-as catalyst activator. 'r- I'hjS feed must be substantially -anhydrous and may-if necessary be dehydrated by. suitable methodsprior. to its K introduction into Another object is to provide other object is to provide for the use of mobile: f 'isomerization catalysts. A still further object a to provide for the recovery and/or re eneratidn chamber it. The hydrogen chloride may be introduced into the reaction chamber in other ways if desired. The feed in line 52 is heated to the proper temperature by means not shown. Suitable temperature and pressure conditions at the inlet of chamber is are 300 F. and 150 lb. per. sq. in. gage. A flow rate of 0.1 to 2.0 liquid vol-- umes oftbuta-ne' per volumeof catalyst chamber per. hour may be used, andtcomplet'e equilibrium conversion in one pass is not ordinarily attempted 1131751101! a process, the hydrocarbon effluents comprising from 25 to 50 per cent isobutane, depending'upon the new rate used.

.The catalyst composition employed comprises a fluid-melt of aluminum chloride with sodium and :rpotassium; ch'l'orided or with halides of other low" .melting metals... The molar ratio of aluminum chionuete the alkali metal chloride should be at least about 1.2 to 1, and greater ratios are ad- We have now found thatthetendencies-towardchangein reactionmate caused-bythe varying re- 5 vantageous. The catalyst composition is promotedby a halide of one of the group Vmetals or a halide of. one oi the sulfur-group elements of greuplVI oi the periodic system. The fluid catalystv flows through condui't'lfi, and is introduced. into reaction chamberjlll at a plurality of points through conduits l5} SIZE}, 22, 2d, 23, and ESL It will be understood that more or fewer such conduits may be used, as required by the particular reaction chamber and conversion taking place therein. The catalyst thus introduced into chamber l6 flows downward over the packing material therein, thus presenting an extended surface. to'the upwardly flowing gases. It will be seenithatin thismethod-of operating, the amount of catalyst increases as it flows down the column iii, which in turnflmeansthat as thereactants flow upward. through the column they contact progressively smaller amounts of catalyst.

. As the reactants pass through the reaction chamber, the normal butane is isomerized to isobutane with the evolution of heat. Such heat of reacti'onis difficult to remove from the large reactor, andas aconsequence the temperature of thegases rises asthey pass upwardly through the reaction chamber ii]. the outlet thereof is accordingly appreciably higher than at the inlet; .the exact temperature difference, of course, varying with the particular chamber, type of reaction, flow rate, extent of reaction-etc. In many cases this temperature dif ference will amount to from 15 to 50 or 60 F. or even more. Such an increase in temperature tends to increase the reaction rate, and in the ordinary..methods of isomerization wherein the reactants are passed througha. uniform bed of catalyst, the reaction frequently runs-away and isdifiicult to bring under control. Increased re action. ratedue to increased temperature causes an-increasedarateoi heat evolution which inturn tendstoincrease. the temperature still more. EX- cessive temperatures. caused by such action cause cracking and oth-erundesirabl e degradation of thebutane undergoing reaction, with consequent lossof material, increased-,fractionation load from light-gases so-formed, and damage tothe catalyst.

. Suchanuncontroliedtemperature rise is obviated-incur. process, due to the: fact that as the temperature rises thereactants are contacted with less and-lesscatalyst The amount of the catalyst at allpoints in the reaetionchamber is correlated, with the temperature prevailing at eachofsaidpoints,bycontrolling the amount of catalyst introduced through eachof the catalyst conduits alongithecha-mber and thus the extent of reaction isli-mited so that in spite of increas- The temperature at ing temperature, a, substantially constant rate of reaction may readily be maintained throughout the reaction zone if desired. Another advantage is that thelimited contact with catalyst of the hottest reactants avoids an undue amount of cracking, so that the isomerization reaction continues at the desired rate while the ratio of cracking to isomerization is less than it would be at the same temperature if the catalyst concentration were higher.

Other varying reaction conditions operating to influence the rate of reaction are the decreasing concentration of normal butane, and the deactivation of the catalyst occurring as it flows through the reaction zone. As the conversion proceeds, the normal butane concentration drops and that of isobutane increases so that mass action effects tend to slow the reaction. In the case just discussed, since equilibrium concentrations, at which all reaction will stop, are not closely approached, this factor is not of so much importance, although it must be taken into account in correlating the catalyst activity at points throughout the column with the reaction conditions. The rate of deactivation of the catalyst as it flows through the chamber will depend upon temperature, amount of excess aluminum chloride in the melt, flow rate of reactants, etc. We have found that the countercurrent flow of catalyst and reactants, with multipoint injection of fresh catalyst, has advantage in that the fresh feed is contacted with a relatively large volume of catalyst which is diluted somewhat with spent catalytic material. This is opposite to the ordinary process with concurrent flow of catalyst and reactants, in which the reactants first contact completely fresh catalyst, and our method, even though the total catalyst activity at the point of first contact with reactants may, as in the case described in conjunction with Figure 1, be greater than at other points, the dilution effect of some spent catalyst aids in promoting smooth and regular reaction. In many cases, variation of one of the reaction conditions may have an effect on reaction rate opposite to that of another varying reaction condition, and in any particular case, the overall effect of the various reaction conditions must be taken into account and correlated with the amount of catalyst introduced at each point.

The isomerization products, which include isobutane, unconverted normal butane, hydrogen chloride, light gases, and traces of C and heavier hydrocarbons, leave chamber l0 via line 30, and are passed to conventional treating and separating means not shown. Ordinarily the isobutane is separated as a product of the process, normal butane and hydrogen chloride are recycled, and light gases may or may not be recycled. Frequently small amounts of hydrogen and/or propane are added to the feed to reduce side reactions, and these gases may be recycled. Certain amounts of propane are formed in the process, and generally separated out from the eiiluents.

The catalyst melt is removed from the bottom of chamber l0 via conduit 32, and most of it is recycled to conduit I4 via line 34 and pump 36. Means other than pumping, such as pressuring with gas, gas-lift, etc. may be used for removing the catalyst melt, and the melt may be heated if necessary by means not shown. A portion of the catalyst stream is passed via line 38 to a purification system indicated diagrammatically at 40. In this purification, completely spent aluminum chloride and other undesirable materials such as I heavy hydrocarbons are removed via line 42, and sufficient fresh aluminum chloride is introduced into the catalyst composition via line 44 to make up for that lost from the process. Catalyst flows from purification 40 to line l4 via line 48.

In Figure 2, the isomerization of normal butane is carried out in the liquid phase, using a slurry of finely divided aluminum chloride as the catalyst. The reaction is carried out continuously by concurrent flow of reactants and catalyst through a series of reactors 50, 52, and 54. A greater or smaller number of such reactors may of course be used as conditions warrant. The hydrocarbon feed, which is predominantly normal butane, is passed in the liquid state from pump 55 at 500 lb. per sq. in. pressure via line 58 through heat exchanger 60, and continues on via lines 52, 66, and HI through heat exchangers 64 and 68 to heater 12, wherein it is brought to the initial reaction temperature, such as 250 F. The thus-heated butane then passes into isomerizer 50 via line 14, admixed with suitable amounts of hydrogen chloride activator from line 16 and catalyst from line 18. The catalyst in line 18 can be a slurry and/or solution of aluminum chloride in liquid hydrocarbons, preferably butane, and is pumped by pump or otherwise forced through the system. A heavy oil. may sometimes be used to advantage in forming this catalyst composition.

The butane, hydrogen chloride, and aluminum chloride are maintained in constant agitation in isomerizer 50 by means of stirrer 82. Isomerizers 52 and 54 are similarly equipped with stirrers 84 and 86. The continuous flow of material into vessel 50 through line 14 causes a continuous flow of hydrocarbons, hydrogen chloride, and catalyst from vessel 50 to vessel 52 via line 88, this material passing through heat exchanger 68 between the two vessels in order to impart heat to the inflowing butane in line 66, being itself cooled to the temperature, around 200 F., required in isomerizer 52. Similarly, material from isomerizer 52 flows to isomerizer 54 via line and heat exchanger 64. A lower temperature, such as F., is maintained in isomerizer 54. It will be understood that by-passes around the heat exchangers may be provided for controlling the temperatures to the desired extent, and auxiliary heating or cooling means may be provided for the incoming butane feed or the flowing reaction mixture as required. a

The isomerizers 50, 52, and 54 are shown to be of the same size as a matter of convenience in the drawing. In actual practice, they may vary in size, depending upon the contact time desired in each of the zones. While any particular molecule of butane may remain in one of the isomerizers for an extremely long or extremely short time, the average time of residence therein is determined by the flow rate of reactants and catalyst and by the volume of the isomerizer.

In the method of operating just described, the

total contact time may be chosen readily so that essentially equilibrium conversion is obtained. Since the equilibrium conversion is greatest at low temperatures, it is desirable to complete the reaction at the lowest convenient temperature at which an economic reaction rate may be obtained. However, to carry out the entire isomerization at such a low temperature would require an unnecessarily long reaction time, and it has been found that the reaction may be initiated at a high temperature, the reactants bemg held at thetiemperatur for at tim s ffici nt.

to obtain considerable isomerization, but limited so that craclring does not occur.

Thus-the first reactor inthe series, isomerizer fit-is maintained at a relatively high temperature. The butane is maintained therein until say so. or 70 percent ofthe equilibrium conversion at that temperatureis obtained, at which time an appreciable amount of undesired cracking is. incipient. At such time,, the reactants leave chamber so andpasson to chamber 52 at a lower temperature, where further conversion is obtainedi.- The flow rate is adjusted so that the residence time at that temperature is suflie cient to obtain additional isomerization but insuflicient to allow cracking. The butane finally passes-to chamber 54 where it is held at the lowest temperature, for additional isomerization, generally until substantially equilibrium conversion is obtained. This method. t operating at a decreasing temperature gradient is now generally known to theindustry, and is described in Lynch U. S. Patent 2,280,710.-

We havefound that by introducing the mobile catalyst-into the reactants at a plurality of points, the amount introduced at each of said points being correlatedwith the particular reacticn oonditionsin the system, a greatly improved operation may be obtained. This is accomplished byintroducing the catalyst; into the reaction mixture not only into line 14; from line 18, but also-into line-83 via line 92 and into line 90 via line 94'. In thisway, the concentration of cata lystin reactants is increased a the reactants pass through the system at a decreasing temperature gradient, The thusrintroduced catalyst also serves to more than. compensate for any catalystdeactivation occurring in the system, and the ratio of catalyst activity to reactants increases in the direction of flow, rather thanremaining constant or decreasing as would be the case in the absence of; the multipoint introduction of the catalyst.

As stated above, the rate of isomerization decreases with decrease in temperature, and this tendency toward. decreased rate is at least partially compensated for by utilization of our inventiompbtaining the advantages of the decreasing; temperature gradient, while substantially def creasing the total time required to effect the desired extent of conversion.

Our invention also acts to at least partially overcome the mass action effects of the isobutane present in the reaction zone. As'the extent of conversion approaches equilibrium, the reaction rate normally tends to decrease, until when equilibrium concentrationsof reactants are attained, further reaction does not occur. Thus, as the reaction mixture flows through. the reaction zones, the reaction rate tends to decrease not only due to the decreasing temperature, but also due to theapproaching Olf equilibrium conditions. In fact, as heretofore explained, the purpose of lowerin the temperature is tozshift the equilibrlum. it will be seen that our invention, by increasing the concentration of catalyst, provides a'means of speeding up the. reaction in spite of increasing concentration of isobutane, which is particularly valuable when the equilibrium percentage of isobutane is slowly approached. Thus, the amount of catalyst introduced at each of. the'points in the system is correlated with tom perature and with concentration of reactants to a compl sh a more i ient co ve ion- The total isomerizationl mixture leaves isom- 'cloride is separated and returned to the system,

erizerts .via line 96 andheat exchanger 60, and passes to separator 98, wherein catalyst is separated from reactantsby gravity settling, centrifuging, filtering, or other means, and is removed, preferably still as a slurry, through line Hi0. Thus all of the catalyst used in the various parts of the apparatus and introduced at the different points is readily removed from the efliuents in a single separation step. The isomerization efiluents comprising isobutane, normal butane, H01, and other light gases, as well as small amounts of C5 and heavier hydrocarbons, pass from separator 98 via line N32 to conventional treatment, separation, etc. not shown. A

portion of the catalyst is recycled to the system from line mil via line l8 and pump 80. Fresh make-up catalyst may be introduced through line iiifii. A portion of the catalyst is taken from line Hill through line 35, and may be sent to'a purification step wherein recoverable aluminum While. spent material such as inactive aluminum chloride-hydrocarbon complexes and other undesirable matter is removed from the system.

The invention has been described with particu lar reference to aluminum chloride catalysts. However, it is to be understood that it is in nowise limited thereto, and may be used in conjunction with other mobile isomerization catalysts. Other aluminum halides, particularly aluminum bromide, and various other metal halide isomerization catalysts of the Friedel- Crafts type may be used. Ordinarily halogenccntaining promoters, such as hydrogen chloride; hydrogen bromide, etc, or other promoters are used with such catalysts.

While hydrogen fluoride may be used as a pr0- motor for the active metal halide catalysts, it has been found that hydrogen fluoridealone is a very active and versatile isomerization catalyst. Thus the isomerization catalyst used in our invention may comrise essentially hydrogen ,iluoride, for example, liquid concentrated or substantially anhydrous hydrogen fluoride, or gaseous hydrogen fluoride. The usefulness of this particular catalyst is realized in view of the fact that it may be used in either the liquid or the vapor phase, in contact with liquid or vaporous hydrocarbons.

In the liquid phase it may pass concurrently with or counter-currently to liquid and/or gaseous hydrocarbons, and in the vapor phase it may pass concurrently with gaseous or liquid hydrocarbons.

or countercurrently to, liquid hydrocarbons.

Thus the particular mode of operating withhy drogen fluoride asgan isomerization catalyst is readily chosen to conform with the hydrocarbons undergoing treatment and with the conversion desired. By the multipcint injection of the hydrogen fluoride into the reaction zone, the total catalytic activity is varied from point to pointin the reaction zone in inverse ratio to the normal variations of reaction rate from point to point, thus establishing a more desirable reaction rate throughout the zone.

While we have discussed our invention in some detail. presented. various modes ofoperation. it. is not limited to the exact variants shown, but is subject to numerous other modifications. For example, mixtures of fresh or regenerated catalyst along with partially or totally spent catalyst React-ants, diluents, heat carriers, and the. like may be used along with the catalyst. These and many other modifications may be utilized in conjunction with the invention, which is to be limited only by the appended claims.

We claim:

1. A process for the isomerization of normal butane to isobutane under conditions of decreasing temperature, decreasing concentration of reactants, and normally decreasing activity of catalyst which comprises passing liquid hydrocarbons comprising normal butane admixed with effective amounts of hydrogen chloride and finely divided aluminum chloride catalyst through a reaction zone, maintaining a decreasing temperature gradient in the direction of flow of said hydrocarbons and said catalyst, maintaining a fiow rate such that the time of residence of said hydrocarbons at any temperature level is sufiicient to effect substantial isomerization but insulhcient to permit any substantial cracking, and such that the final temperature level is sufii'ciently low to obtain a concentration of isobutane in excess of the equilibrium concentration thereof at the highest temperature level, and introducing a separately controlled quantity of said finely divided aluminum chloride catalyst into said liquid hydrocarbons at each. of a plurality of points along the direction of fiow sufiicient to more than overcome deactivation of catalyst which would normally occur in the absence of the catalyst thus introduced at said plurality of points and sulficient to increase the ratio of catalyst activity to hydrocarbons along the direction of flow, thereby establishing a constant rate of reaction throughout the reaction zone despite said decreasing temperature gradient, decreasing concentration of normal butane, and normally decreasing catalyst activity.

2. A process for the isomerization of normal butane under conditions of decreasing temperature, decreasing concentration of reactants, and normally decreasing activity of catalyst to isobutane which comprises passing a liquid hydrocarbon feed comprising normal butane in indirect heat exchange at a plurality of points with a warmer reaction mixture flowing in a reaction zone in an opposite direction to heat said feed and to cool the reaction mixture as it flows through said reaction zone, admixing with thusheated feed effective amounts of hydrogen chloride and a finely divided aluminum chloride catalyst composition hereinafter described to form said reaction mixture, passing same at isomerization conditions through said reaction zone in indirect heat exchange with said feed as aforesaid thereb maintaining a decreasing temperature gradient in the direction of flow of said reaction mixture, maintaining a flow rate through said reaction zone such that the time of residence of said hydrocarbons within each temperature range is sumcient to efiect substantial isomerization but insufficient to permit any substantial cracking, maintaining the final reaction temperature of said reaction mixture sufllciently low to obtain a concentration of isobutane in excess of the equilibrium concentration thereof at the highest temperature range, separating said catalyst from effluents of said reaction zone, discarding a portion of the thus-separated catalyst and adding fresh makeup catalyst to the balance to control the activity thereof, introducing a portion of said catalyst composition of controlled activity into the heated feed as aforesaid in a controlled quantit and sufiicient to effect some isomerization but insuificient to effect the total isomerization in said reaction zone within the dethe reaction zone despite said decreasing temperature gradient, decreasing concentration of normal butane, and normally decreasing catalyst activity.

3. A process for the isomerization of a first saturated hydrocarbon into an isomer thereof having the same molecular weight and whose concentration in an equilibrium mixture with said first saturated hydrocarbon increases with decreasing temperature, said process being effected under conditions of decreasing temperature, decreasing concentration of reactants, and normally decreasing activity of catalyst, which comprises passing liquid hydrocarbons comprising said first saturated hydrocarbon admixed with effective amounts of a mobile Friedel-Craits type metal halide isomerization catalyst through a re action zone, maintaining a decreasing tempera.

ture gradient in the direction of fiow of said hydrocarbons and said catalyst, maintaining a fiow rate such that the time of residence of sai" hydrocarbons at any temperature level is sufficient to effect substantial isomerization but insuificient to permit any substantial cracking and such that the final temperature level is sufiiciently low to obtain a concentration of said isomer in excess of the equilibrium concentration thereof at the highest temperature level, and introducing a separately controlled quantity of said isomerization catalyst into said liquid hydrocarbons at each of a plurality of points along the direction of flow sufiicient to more-than overcome deactivation of catalyst which would normally ocour in the absence of the catalyst thus introduced at said plurality of points and sufiicient to increase the ratlo of catalyst activity to hydrocarbons along the direction of flow, thereby establishing a constant rate of reaction throughout the reaction zone despite said decreasing temperature gradient, decreasing concentration of said first saturated hydrocarbon, and normally decreasing catalyst activity.

4. The process of claim 3 in which said catalyst comprises an aluminum halide.

5. The process of claim 3 in which said catalyst comprises aluminum chloride.

THOMAS B. HUDSON. JOHN D. UPHAM.

REFERENCES CITED The following references are of record in the file of this patent:

UNITED STATES PATENTS Number Name Date 1,870,792 Clark Aug. 9, 1932 1,981,305 Bray et a1. Nov. 20, 1934; 2,280,710 Lynch .Apr. 21, 1942 2,283,143 Ipatiefi et a1. May 12, 1942 2,283,852 Egloff May 19, 1942 2,325,052 Grosse et al July 27, 1943 2,342,124 Danforth Feb. 22, 1944 2,343,406 Dryer Mar. 7, 1944 2,349,516 Pines et a1 May 23, 1944 t Certificate of Correction Patent No. 2,439,301. April e, 1948. THOMAS B. HUDSON ET AL.

It is hereby certified that error appears in the printed specification of the above numbered patent requiring correction as follows: Column 9, lines 41 and 42, claim 2,

strike out the words to isobutane and insert the same in line 39, same claim, after butane; and that the said Letters Patent should be read with this correction therein that the same may conform to the record of the case in the Patent Office.

Signed and sealed this 22nd day of June, A. D. 1948.

THOMAS F. MURPHY,

Assistant aonwm'asioner of Patents. 

